Exxonmobil Research and Engineering Company

Exxonmobil Chemical Patents Inc.

Other

Exxon Mobil Chemical, Inc.

Jennifer Schaefer Feeley

Stuart Leon Soled

James C Vartuli

Sabato Miseo

Robert J Wittenbrink

Joseph Ernest Baumgartner

Charles John Mart

Christine Esther Kliewer

Janet Renee Clark

Steven T Ragomo

Richard Henry Schlosberg

Shifang Luke Luo

Sebastian Carmen Reyes

Andrzej Mariusz Malek

Frank Hershkowitz

Harry William Deckman

Paul Joseph Berlowitz

Wenyih Frank Lai

John Scott Buchanan

Gabor Kiss

Jane C Cheng

Chuansheng Bai

Andrzej Malek

John Frances Brody

Lanny D Schmidt

Gary L Casty

Hyung Suk Woo

John Henry Dunsmuir

Mark Leland Tiller

Bruce Derites

Jeffrey M Dysard

Keith L Hohn

Ioannis P Androulakis

Andrzel Malek

Sal Miseo

Robert Jay Wittenbrink

James Clarke Vartuli

The present invention is directed to a process for hydrogenating one or more organic compounds especially unsaturated organic compounds by bringing the compound into contact with a hydrogen-containing gas in the presence of a catalyst, which comprises one or more catalytically active metals applied to a porous catalyst support. The one or more catalytically active metals having been derived via a decomposed organic complex of the metal on the support, in particular amine complexes of the metal. The decomposed complex may be treated with hydrogen to activate the catalyst before use as a hydrogenation catalyst.

Hydrogenation processes

A substantially surface-deactivated catalyst composition that is stable at least to 300&#xb0; C. The catalyst includes a zeolite catalyst (e.g., ZSM-22, ZSM-23, or ZSM-57) having active internal Br&#xf6;nsted acid sites and a surface-deactivating amount of a rare earth or yttrium oxide (e.g., chosen from lanthanum oxide or lanthanides oxide). This catalyst is preferably used in a process for producing a higher olefin by oligomerizing a light olefin, wherein the process includes contacting a light olefin under oligomerization conditions with the substantially surface-deactivated catalyst composition.

Lightly branched higher olefin oligomerization with surface modified zeolite catalyst

The present invention is directed to processes for preparing supported metal catalysts comprising one or more catalytically active metals applied to a porous catalyst support and to processes that use such catalysts. The process requires the formation of an organic complex during the manufacture of the catalyst which after its formation is either partially or fully decomposed before reduction if the metal to form the catalyst. The catalysts have high levels of metal dispersion and uniform distribution of catalytically active metals on the support. The catalysts obtained form the processes are particularly effective in catalysing Fischer-Tropsch reactions and as adsorbants for the removal or organosulfur compounds from hydrocarbons.

Methods for preparing catalysts

A multistage catalytic partial oxidation (CPO) process for oxidizing a hydrocarbon feedstream comprising C -C hydrocarbons, with an oxygen-containing feedstream to produce a product comprising CO and H , also known as synthesis gas or syngas. The process employs a CPO catalyst, and controlled process features, including: (A) the total oxygen requirement for the process is introduced incrementally, in more than one reaction stage, using an oxygen-containing feedstream at more than one feed point in the process, each stage including a catalyst; (B) the oxygen-containing feedstream, hydrocarbon feedstream and, in reaction stages after the first of said multiple stages, the intermediate product produced in the prior stage, are mixed for a period of time, after they are brought into contact with one another, of less than about 1 millisecond to form a substantially uniform mixture, wherein the mixture is then contacted with the catalyst; (C) the oxygen-containing feedstream and the hydrocarbon feedstream are preheated prior to entry into the first stage, to a temperature of from about 450&deg; C. to less than about 1,000&deg; C.; and (D) the mixture temperature of the product in each stage following the first stage is from greater than about 600&deg; C. to less than about 1,000&deg; C. Preferably, the process comprises less than or equal to about five stages, the first stage preheat temperature recited in step (C) is greater than about 550&deg; C. and the mixture temperature of the product in each stage following the first stage is at least 700&deg; C.

Catalytic partial oxidation using staged oxygen addition

A slurry Fischer-Tropsch hydrocarbon synthesis process for synthesizing liquid hydrocarbons from synthesis gas in a synthesis reactor also hydroisomerizes the synthesized hydrocarbon liquid, which comprises the slurry liquid, in one or more lift reactors immersed in the slurry body in the synthesis reactor. A monolithic catalyst is preferably used for the hydroisomerization, and slurry circulation up through the lift reactors from the surrounding slurry body, is achieved at least in part by the lift action of the hydroisomerization treat gas. Preferably, catalyst particles are also removed before the slurry contacts the catalyst. Hydroisomerization occurs while the synthesis reactor is producing hydrocarbons, without interfering with the synthesis reaction. A gas bubble reducing downcomer may be used to produce and feed the gas bubble reduced slurry into the lift reactor, thereby providing a hydraulic head assist in the slurry circulation up through and out of the lift reactor.

Slurry hydrocarbon synthesis with liquid hydroisomerization in the synthesis reactor

A slurry Fischer-Tropsch hydrocarbon synthesis process for synthesizing liquid hydrocarbons from synthesis gas in a synthesis reactor also hydroisomerizes the synthesized hydrocarbons in one or more external lift reactor hydroisomerizing loops outside of the reactor, but which are a part of the reactor. A monolithic catalyst is used for the hydroisomerization and slurry circulation between the synthesis reactor and one or more loops is achieved, at least in part, by the lift action of a hydrogen treat gas injected into each loop.

Slurry hydrocarbon synthesis with isomerization zone in external lift reactor loop

A slurry Fischer-Tropsch hydrocarbon synthesis process for synthesizing liquid hydrocarbons from synthesis gas, in a hydrocarbon synthesis reactor, also hydroisomerizes the synthesized hydrocarbons in one or more external downcomer reactor hydroisomerizing loops outside of the reactor, but which are a part of the synthesis reactor. A monolithic catalyst is used for the hydroisomerization, and slurry circulation between the synthesis reactor and the one or more hydroisomerization loops is achieved, at least in part, by density-difference driven hydraulics created by removing gas bubbles from the slurry passed into the loop. Preferably, catalyst particles are also removed before the slurry contacts the monolithic hydroisomerization catalyst.

Slurry hydrocarbon synthesis with external hydroisomerization in downcomer reactor loop

A slurry Fischer-Tropsch hydrocarbon synthesis process for synthesizing liquid hydrocarbons from synthesis gas in a hydrocarbon synthesis reactor also hydroisomerizes the synthesized hydrocarbon liquid, which comprises the slurry liquid, in one or more downcomer reactors immersed in the slurry body in the synthesis reactor. A monolithic catalyst is preferably used for the hydroisomerization, and slurry circulation down through the downcomer reactors from the surrounding slurry body, is achieved at least in part by density-difference driven hydraulics created by removing gas bubbles from the slurry passed into the downcomers. Preferably, catalyst particles are also removed before the slurry contacts the catalyst. Hydroisomerization occurs while the synthesis reactor is producing hydrocarbons, without interfering with the hydrocarbon synthesis reaction.

In-situ hydroisomerization of synthesized hydrocarbon liquid in a slurry fischer-tropsch reactor

Catalytic partial oxidation is effected in the presence of a supported, Group VIII metal catalyst by reacting a light hydrocarbon with an oxygen containing gas, the catalyst support being in a preferred size range.

Catalytic partial oxidation &mdash; particulate catalysts

A process for the partial catalytic oxidation of a hydrocarbon containing feed comprising contacting the feed with an oxygen-containing gas in the presence of a catalyst retained within a reaction zone in a fixed arrangement, wherein the catalyst comprises at least one catalytically active metal selected from the group consisting of silver and Group VIII elements supported on a porous ceramic carrier. The porous ceramic carrier has a distribution of total pores wherein about 70% of the total pores (1) have a volume-to-surface area (V/S) ration that is within about 20% of the mean V/S value for the total pores and no pores have a V/S ration that is greater than twice the mean V/S value for the total pores; (2) have a pore-to-pore distance between neighboring pores that is within about 25% of the mean pore-to-pore distance between neighboring pores; and (3) have a pore throat area that is within about 50% of the mean pore throat are for the pores. Additionally, about 50% of the total pores have a coordination number between neighboring pores that is within about 25% of the mean coordination number between neighboring pores. Preferably, the oxidation process comprises a multistage, staged oxygen, catalytic partial oxidation process having fewer than or equal to about five stages and including a first stage preheat temperature of greater than about 550&deg; C., and wherein the temperature of the product mixture in each stage following the first stage is at least about 700&deg; C.

Catalytic oxidation process

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Lebanon, NJ, United States of America

Jennifer Schaefer Feeley